Method for producing conductive masterbatch
a technology of conductive masterbatch and conductive ether, which is applied in the direction of non-metal conductors, conductors, transportation and packaging, etc., can solve the problems of die drip, poor moldability of polyphenylene ether, and large quantity of conductive masterbatch production, etc., to achieve excellent conductivity, reduce resin temperature, and increase the output of extruding
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[0137]Hereinbelow, the present invention will be described in more detail with reference to the following Examples and Comparative Examples.
(Raw Materials Used)
(1-1) Polyamide 6 pellet (hereinafter, may be abbreviated to “PA6-1”)
[0138]Unitika nylon A1020BRL (manufactured by Unitika, Ltd.)
(1-2) Polyamide 6 powder (hereinafter, may be abbreviated to “PA6-2”)
[0139]Unitika nylon A1020LP (manufactured by Unitika, Ltd.)
(2-1) Polyamide 66 (hereinafter, may be abbreviated to “PA66-1”)
[0140]Viscosity number: 120 (measured in 96% sulfuric acid according to ISO 307)
[0141]Concentration of terminal amino groups: 20 micromol / g
[0142]Concentration of terminal carboxyl groups: 110 micromol / g
[0143]Pellet shape: Average pellet length: 3 mm, Average diameter of pellet cross-section: 2 mm
[0144]Water content: 1,500 ppm (determined at a furnace temperature of 185° C. using a Karl Fischer water determination device)
[0145](2-2) PA66-1 was melted in the ZSK40MC extruder set at 280° C. and pelletized using a ...
examples 1 and 2
[0161]There was prepared a TEM58SS extruder (manufactured by Toshiba Machine Co., Ltd.) having inlets at least at three places, an upstream portion, an intermediate portion, and a downstream portion, of the extruder, and an open vent equipped in the further downstream of the inlet at a downstream portion. As a screw configuration of the extruder, one kneading zone was provided between the inlet at an upstream portion and the inlet at an intermediate portion, and two kneading zones were provided between the inlet at a downstream portion and a place just before a die. The cylinder temperature of the extruder between the inlet at an upstream portion and a place just before the inlet at an intermediate portion was set at 280° C.; the cylinder temperature between the inlet at an intermediate portion and a place immediately before the die was set at 260° C.; and the temperature of the die was set at 330° C.
[0162]At a proportion given in Table 1, 50 parts by mass of PA66-1 were fed through...
examples 3 to 5
[0166]These Examples were carried out in substantially the same manner as in Example 2 except that the ratio of the polyamide fed through the inlet at an upstream portion to that fed through the inlet at a downstream portion was changed to the ratios given in Table 1. In Example 3, strand breakage did not occur, and the extrusion was favorable. However, a formation of some die drips was observed at the die lip part. Further, in Examples 4 and 5, a phenomenon was observed in which the torque and resin temperature during extrusion increased, and it was found that the occurrence of strand breakage and formation of die drips tended to increase, as the ratio of the polyamide fed through the inlet at an upstream portion is increased. Furthermore, in Example 3, the maximum stable output of extruding was 420 kg / h which is the feeding limit output of extruding of CB as in Examples 1 and 2, and it was impossible to measure the output of extruding at the 85% torque. On the other hand, in Examp...
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Abstract
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